EP0451614B1 - Catalyseur fluide pour utilisation dans l'oxidation gazeuse d'hydrocarbures aromatiques - Google Patents

Catalyseur fluide pour utilisation dans l'oxidation gazeuse d'hydrocarbures aromatiques Download PDF

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EP0451614B1
EP0451614B1 EP91104826A EP91104826A EP0451614B1 EP 0451614 B1 EP0451614 B1 EP 0451614B1 EP 91104826 A EP91104826 A EP 91104826A EP 91104826 A EP91104826 A EP 91104826A EP 0451614 B1 EP0451614 B1 EP 0451614B1
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catalyst
oxide
weight
component
source
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EP0451614A1 (fr
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Toshinao C/O Chiba Works Aono
Yukio C/O Kawasaki Steel Corporation Asami
Noboru C/O Kawasaki Steel Corporation Hirooka
Yusaku Arima
Susumu Fujii
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JFE Steel Corp
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Kawasaki Steel Corp
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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
    • C07C51/16—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation
    • C07C51/21—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen
    • C07C51/255—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of compounds containing six-membered aromatic rings without ring-splitting
    • C07C51/265—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of compounds containing six-membered aromatic rings without ring-splitting having alkyl side chains which are oxidised to carboxyl groups
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J23/20—Vanadium, niobium or tantalum
    • B01J23/22—Vanadium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
    • B01J27/02—Sulfur, selenium or tellurium; Compounds thereof
    • B01J27/053—Sulfates
    • B01J27/055—Sulfates with alkali metals, copper, gold or silver
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/30—Catalysts, in general, characterised by their form or physical properties characterised by their physical properties
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/40—Catalysts, in general, characterised by their form or physical properties characterised by dimensions, e.g. grain size
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
    • B01J35/61—Surface area
    • B01J35/613—10-100 m2/g
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
    • B01J35/63—Pore volume

Definitions

  • This invention relates to fluid catalysts for use in the production of carboxylic anhydrides from aromatic hydrocarbons. More particularly, it relates to a fluid catalyst for use in the production of phthalic anhydride from a hydrocarbon material such, especially, as o-xylene or naphthalene by means of gas phase oxidation. It also relates to a process for the production of the fluid catalyst.
  • Carboxylic anhydrides are produced by gas phase oxidation of aromatic hydrocarbon materials, with a typical example being the production of phthalic anhydride from o-xylene or naphthalene.
  • a catalyst in which active components are coated on an inert carrier is apt to cause a run-away reaction triggered by non-uniformity of reaction due to channeling of reaction gas, formation of hot spots, increased pressure loss and the like caused by peeling and release of the active components from the carrier during packing of the catalyst or at the time of the operation.
  • high productivity cannot be attained by the use of the fixed bed process because concentration of a reaction gas must be maintained within its explosion limit and, therefore, the reaction gas can be supplied only at a low concentration level.
  • a number of catalysts in which titanium oxide is used as a carrier and vanadium pentoxide is supported on the carrier have been proposed for example in B.P. 1,067,726 (1967) and Fr.P. 1,537,351 (1968).
  • a catalyst having certain mechanical strength can be obtained by making a fused body of titanium oxide and vanadium pentoxide together with ammonium thiocyanate or an alkali compound.
  • specific surface area and pore volume of the catalyst decrease by the formation of fused body, thus resulting in significant reduction of the catalytic activity. Because of the reduced activity, such a fused catalyst requires a high reaction temperature which causes excess oxidation and side reactions. In consequence, it is difficult to obtain phthalic anhydride with a high yield by the use of the fused catalyst.
  • a catalyst for use in a fluidized bed process for the production of phthalic anhydride from o-xylene or naphthalene by means of a gas phase oxidation reaction a process which is greatly advantageous compared to a fixed bed process, as well as to provide a process for the production of such a fluid catalyst.
  • a more specific object of the present invention contemplates the provision of a high activity and high selectivity catalyst for use in a fluidized bed process, in which a mixture of titanium oxide, silicon dioxide and boron oxide is used as a support or carrier and which has sufficient strength and appropriate bulk density.
  • the inventors of the present invention have conducted intensive studies on the development of a fluid catalyst containing titanium oxide as the main component, which is useful for the production of phthalic anhydride. This invention has been accomplished as a result of these efforts.
  • a fluid catalyst for use in gas phase oxidation of aromatic hydrocarbons comprising 50 to 95% by weight (calculated by TiO2 + SiO2 + B2O3) of component (A) which comprises titanium oxide, silicon dioxide and boron oxide and 5 to 50% by weight [calculated by V2O5 + M2O (M represents an alkali metal) + SO3] of component (B) comprising vanadium oxide, an alkali metal oxide and sulfuric anhydride, wherein said V2O5 in the catalyst is in the range of from 1 to 30% by weight when the component (A) is calculated by TiO2 + SiO2 + B2O3, weight ratios of B2O3 to TiO2 and SiO2 to TiO2 in said component (A) are in the range of from 0.02 to 0.5 and from 0.25 to 1.0, respectively.
  • component (B) when component (B) is calculated by V2O5 + M2O + SO3, molar ratios of SO3 to M2O and M2O to V2O5 in said component (B) are in range of from 0.1 to 6.0 and from 0.1 to 5.0, respectively.
  • a process for the production of a carboxylic anhydride which comprises performing gas phase oxidation of an aromatic hydrocarbon in the presence of the fluid catalyst.
  • a fluid catalyst of the present invention for use in gas phase oxidation of aromatic hydrocarbons comprises: 50 to 95% by weight (calculated by TiO2 + SiO2 + B2O3) of component (A) which comprises titanium oxide, silicon dioxide and boron oxide and 5 to 50% by weight [calculated by V2O5 + M2O (M represents an alkali metal) + SO3] of component (B) comprising vanadium oxide, an alkali metal oxide and sulfuric anhydride, wherein weight ratios of B2O3 to TiO2 and SiO2 to TiO2 in the component (A) are in the range of from 0.02 to 0.5 and from 0.25 to 1.0, respectively.
  • Amounts of the component (A) as a carrier in the catalyst if smaller than 50% by weight may not be preferable, because a catalyst having an appropriate bulk density which is suitable for use in a fluidized bed process will not be obtained and the activity of the catalyst will decrease. If amounts of the component (A) are larger than 95% by weight, amounts of the component (B) which is the source of active components in the catalyst will conversely be reduced and, therefore, a desired catalytic activity will not be obtained.
  • Preferable amount of the component (A) in the catalyst may be in the range of from 60 to 90% by weight, more preferably from 75 to 90% by weight.
  • a weight ratio of B2O3 / TiO2 is in the range of from 0.02 to 0.5, preferably from 0.05 to 0.3, and that of SiO2 / TiO2 is in the range of from 0.25 to 1.0, preferably from 0.3 to 0.9.
  • the B2O3 / TiO2 weight ratio is smaller than 0.02, effects of the addition of boron oxide on the improvement of abrasion resistance and selectivity for reaction products of the catalyst will not be attained.
  • the weight ratio if larger than 0.5 may not be preferable, because the catalytic activity will decrease markedly, though the effect on the improvement of abrasion resistance will not decrease.
  • the SiO2 / TiO2 weight ratio is smaller than 0.25, bulk density of the resulting catalyst will increase and, therefore, a catalyst suitable for use in a fluidized bed process will not be obtained.
  • the weight ratio if larger than 1.0 may not be preferable, because specific surface area of the resulting catalyst will become large and selectivity of the catalyst will decrease.
  • the component (B) as active component in the catalyst is used in an amount of from 5 to 50% by weight, preferably from 10 to 40% by weight, more preferably from 10 to 30% by weight, calculated by a form of "V2O5 + M2O (M is an alkali metal) + SO3".
  • Vanadium compound as a member of the component (B) is contained in the catalyst in an amount of from 1 to 30% by weight, more preferably from 1 to 15% by weight, calculated by a form of V2O5.
  • a molar ratio of SO3 to M2O is in the range of from 0.1 to 6.0, preferably from 1.0 to 4.0, and a molar ratio of M2O to V2O5 (M2O/V2O5) is in the range of from 0.1 to 5.0, preferably from 0.3 to 3.0.
  • the fluid catalyst for gas phase oxidation use may further contain a third component such as a rare earth compound in addition to the components (A) and (B).
  • a third component such as a rare earth compound in addition to the components (A) and (B).
  • a process for the production of a fluid catalyst containing titanium oxide, silicon dioxide, vanadium oxide, an alkali metal oxide, sulfuric anhydride and boron oxide as main components which comprises the steps of
  • the material for use in the production process of a catalyst of the present invention is a solution or a suspension of respective sources of titanium oxide, silicon dioxide, vanadium oxide, an alkali metal oxide, sulfuric anhydride and boron oxide.
  • the source of titanium oxide eligible for use in the present invention is a titanium hydroxide which is capable of forming titanium oxide having a crystallite diameter of not more than 30 nm when dried at a temperature of about 300°C.
  • a catalyst containing titanium oxide which has a crystallite diameter of larger than 30 nm may have markedly low abrasion resistance compared to that having a crystallite diameter of not more than 30 nm.
  • the use of such a catalyst containing large crystallite diameter titanium oxide in a fluidized bed system therefore, will result in the discharge or scattering of the catalyst to a high degree which is not only uneconomical but also causes blocking of the tubes of a cyclone and a heat exchanger. Also, the use of such a catalyst will cause mixing of a large amount of the catalyst into a reaction product and also will make it difficult to keep a reaction gas in a proper state of fluidity.
  • a titanium hydroxide which is capable of forming titanium oxide having a crystallite diameter of not more than 30 nm when dried at a temperature of about 300°C is intended to include not only wet (water containing) titanium compounds which are cenerally called titanium hydroxide, metatitanic acid, orthotitanic acid, titania sol, titania gel and the like but also powder preparations obtained by drying them at a low temperature.
  • a titanium oxide source (or titanium hydroxide) eligible for use in the present invention may be obtained from any material or by any preparation method.
  • the titanium dioxide source in powder form has after drying at about 300°C a crystallite diameter of no more than 30nm, more preferably 20nm or smaller and most preferably of 10 nm or smaller.
  • titanium oxide examples include a titanic acid which is obtained by thermal hydrolysis during an intermediate step of a process for the production of titanium oxide for pigment use, and a titania sol preparation which is obtained by adding an acid to the titanic acid. Also included are titanium hydroxides, titania sol preparations and the like which are obtained by means of a neutralization hydrolysis or an ion exchange deoxidation hydrolysis of titanium sulfate, titanyl sulfate, titanium tetrachloride and the like.
  • a titanium hydroxide obtained from a solution of titanyl sulfate or the like by means of a neutralization hydrolysis at a low temperature of 40°C or below may be most useful as a material for the production of a catalyst of the present invention, because its crystallite diameter when dried at about 300°C is only several nm.
  • a source of silicon dioxide is used as a lightening agent (or a bulk density reducing agent) and as a binder.
  • a desirable material as the source of silicon dioxide eligible for use in the present invention may be in the form of a solution or silica sol which has a good dispersion ability. Examples of such desirable material include for instance a silicic acid which is obtained by subjecting a sodium silicate or a potassium silicate to a neutralization or a cation exchange method, organic silicon compounds such as an ethyl silicate and acid hydrolyzates thereof, a quaternary ammonium silicate and an acid hydrolyzate thereof, colloidal silica and the like.
  • colloidal silica is most preferable because of its stability at a high concentration for a long period of time.
  • a colloidal silica preparation contains sodium as a stabilizer, it is preferable to remove sodium in advance by means of cation exchange, ultrafiltration or the like.
  • a colloidal silica preparation having a particle size of 50 nm or larger may be useful as a bulk density reducing agent, but it has an inferior capacity as a binder.
  • Gel-form materials such as a hydrogel obtained by neutralizing a sodium silicate and powdered gel preparations including a white carbon and an aerogel, are not preferable as the source of silicon dioxide because such materials not only have poor dispersion ability and inferior capacity as a binder but also reduce the catalytic effect of simultaneously added boron compound (or boron oxide).
  • a source of vanadium oxide eligible for use in the present invention may be selected from water soluble compounds which form vanadium oxide when calcinated in the air, such as ammonium metavanadate, vanadyl sulfate (or vanadium oxysulfate), vanadium formate, vanadium acetate, vanadyl oxalate, ammonium vanadium oxalate, vanadyl phosphate, a vanadium oxyhalide and the like.
  • vanadyl sulfate, ammonium metavanadate and vanadyl oxalate may preferably be used.
  • Examples of the source of alkali metal oxide eligible for use in the present invention include hydroxides, sulfates, carbonates, chlorides, nitrates, oxihalides, thiosulfates, nitrites, sulfites, hydrogensulfites, hydrogensulfates, oxalates, hydrogenoxalates and the like of potassium, cesium, rubidium and other alkali metals.
  • hydroxides, sulfates and carbonates may be used preferably.
  • sulfuric acid compounds as the source of sulfuric anhydride include sulfuric acid, ammonium sulfate, ammonium hydrogensulfate and the like. Of these, sulfuric acid and ammonium sulfate may be used preferably.
  • such a vanadium compound, an alkali metal compound and a sulfuric acid compound are used as active components.
  • a boron compound eligible for use in the present invention as the source of boron oxide may be selected from soluble compounds such as boron oxide, boric acid, potassium tetraborate, potassium pentaborate, potassium metaborate, ammonium metaborate, ammonium tetraborate and the like, preferably from boric acid and ammonium metaborate because of their relatively high solubilities.
  • a boron compound (or boron oxide) imparts not only an effect of improving strength of catalyst (abrasion resistance) markedly but also an effect of improving selectivity for the reaction products.
  • a catalyst may have excellent activity, selectivity and abrasion resistance when it is produced by using active components and a titanium hydroxide which is capable of forming titanium oxide having a crystallite diameter of not more than 30 nm when dried at about 300°C.
  • strength of the catalyst and selectivity for the reaction products of the catalyst are further improved by the effect of the use of a boron compound in spite of the accelerated formation of titanium oxide crystals at the time of calcination of the catalyst composition.
  • the process for the production of the catalyst of the present invention comprises steps of mixing the foregoing component materials, spray-drying the mixture and calcinating the spray-dried powder. Since mixing order of each component is optional, various mixing methods may be applicable such as simultaneous dissolving of two or more materials, dissolving of active components in a titanium hydroxide disperse liquid and the like.
  • titanium oxide a mixture of a titanium hydroxide, which is capable of forming titanium oxide having a crystallite diameter of not more than 30 nm when dried, with another titanium compound such as a compound that forms titanium oxide having a crystallite diameter of larger than 30 nm.
  • concentration of a slurry mixture thus prepared may be adjusted to an appropriate level by means of evaporation, prior to subjecting the mixture to the spray drying step to obtain spherical fine particles.
  • the spray drying step may be effected by employing commonly used means.
  • spray drying may be carried out under such conditions that a weight average particle size of the resulting spherical fine particles is controlled within the range of from 40 to 150 ⁇ m.
  • the spherical fine particles thus obtained are then calcinated in the air preferably at a temperature of from 300 to 700°C, more preferably from 400 to 600°C, and preferably for 1 to 6 hours, more preferably for 2 to 4 hours.
  • a catalyst having the following properties may preferably be obtained.
  • abrasion rate is measured by the ACC (American Cyanamid Co.) method described in B.P.737,429.
  • the catalyst obtained in the present invention can be applied preferably to a process for the production of a caboxylic anhydride from a corresponding aromatic hydrocarbon by means of a gas phase oxidation.
  • aromatic hydrocarbons include benzene, xylene, cumene, pseudocumene, durene and mixtures thereof. Consequently, the catalyst obtained by the process of the present invention can be used for the oxidation of: benzene into maleic anhydride, pseudocumene into trimellitic anhydride, durene into pyromellitic anhydride, and o-xylene or naphthalene into phthalic anhydride.
  • a hydrocarbon source for the production of phthalic anhydride by the use of the catalyst of the present invention may be o-xylene, naphthalene, and the like, preferably, o-xylene, more preferably an aromatic hydrocarbon which contains at least 10 mol% or more of o-xylene.
  • a process for the production of phthalic anhydride from o-xylene is described in the following as an illustrative example of the application of the catalyst of the present invention. This example, however, is in no way to be taken as limiting.
  • air may be used preferably as the source of oxygen taking various conditions into consideration, though not specifically restricted.
  • a gas mixture which comprises oxygen and a dilution gas such as a nitrogen/carbon dioxide dilution gas, as well as an air system supplemented with oxygen, may also be useful as the source of oxygen.
  • the oxygen-containing gas source (air for example) may preferably be subjected to a preheating step (for example at 100 to 300°C) prior to introduction into a reactor.
  • the oxidation reaction can be carried out at, over or below the atmospheric pressure. Generally, the reaction may preferably be carried out at an atmospheric pressure of from 0.5 to 3.0. Preferably, the oxidation reaction may be carried out at a reaction temperature of from 300 to 450°C.
  • the catalyst may preferably be used in an amount of from 10 to 30 kg / (kg - material gas / Hr). Preferable ratio of a material air to gas in the reaction gas mixture may be in the range of from 5 to 15 kg/kg.
  • a 600 kg portion of a titanyl sulfate aqueous solution containing 5% by weight of titanium as TiO2 was cooled to 12°C and then neutralized by gradually adding 140 kg of 15% by weight aqueous ammonia spending about 10 minutes with thorough stirring to obtain a titanium hydroxide gel.
  • the thus obtained gel showed a pH value of 8.5 and a temperature of 25°C.
  • a portion of the purified gel was dried at a temperature of 300°C and the resulting powder was subjected to X-ray diffraction.
  • a silica sol article having a mean particle size of 5 nm (Cataloid SI-550, manufactured by Catalysts & Chemicals Industries Co., Ltd.; consult Table 1 for its properties) was passed through a cation exchange resin layer to obtain 200 kg of Na-removed silica sol.
  • the thus obtained Na-removed silica sol contained 10.3% by weight of SiO2 with a Na2O/SiO2 weight ratio of 0.002.
  • a 600 dm3 capacity stainless steel vessel equipped with a steam jacket was charged with the whole amount of the previously prepared gel slurry containing 5.0% by weight of TiO2 and, with stirring, charged further with 97.5 kg of the just described Na-removed silica sol, 7.82 kg of a vanadyl sulfate aqueous solution containing 19.3% by weight of vanadium as V2O5 and 2.36 kg of a cesium sulfate aqueous solution containing 50.0% by weight of cesium as Cs2SO4 in that order. To the resulting mixture was added 0.97 kg of ammonium sulfate crystals and, finally, 80 kg of a previously prepared boric acid aqueous solution (2.8% by weight as H3BO3 concentration). This mixture showed a pH value of 2.5.
  • Example 2 The process of Example 1 was repeated except that the amount of boron oxide was changed to obtain catalyst B, with its chemical composition and physical properties shown in Table 2.
  • Example 2 The process of Example 1 was repeated except that the amount of boron oxide was changed to obtain catalyst C, with its chemical composition and physical properties shown in Table 2.
  • Example 2 The process of Example 1 was repeated except that the source of B2O3 was not used to obtain catalyst D, with its chemical composition and physical properties shown in Table 2.
  • Example 2 The process of Example 1 was repeated except that the amount of boron oxide was changed to the highest level to obtain catalyst E, with its chemical composition and physical properties shown in Table 2.
  • a metatitanic acid slurry which is obtained as an intermediate product of a process for the production of titanium oxide for pigment use, was diluted and subjected to neutralization and washing steps in the same manner as in Example 1 to obtain a titanium hydroxide gel from which sulfuric acid was removed. Concentration of TiO2 in the gel was found to be 29.0% by weight. When a portion of the thus prepared gel was dried at 300°C, the resulting powder showed a crystallite diameter of 16 nm.
  • a powder preparation containing silicon dioxide, active components and boron oxide was prepared from the gel by similar means to the case of catalyst A, and the powder was calcinated at 600°C for 3 hours to obtain catalyst F. Chemical composition and physical properties of this catalyst are shown in Table 2.
  • the titanium hydroxide gel obtained in Example 4 was diluted with pure water to a gel concentration of 15% by weight, and the diluted gel was adjusted to pH 2 with nitric acid.
  • the resulting slurry was heated at 180°C for 100 hours with stirring using an external heating type autoclave. When a portion of the thus heated slurry was dried at 300°C, the resulting powder showed a crystallite diameter of 35 nm.
  • catalyst G having properties as shown in Table 2 was obtained from the thus prepared titanium hydroxide slurry.
  • a commercial article of anatase type titanium oxide powder (A#200, manufactured by Teikoku Kako Co., Ltd.) was suspended in pure water to prepare a slurry containing 30% by weight of titanium as TiO2, and catalyst H having properties as shown in Table 2 was obtained from the thus prepared slurry in the same manner as in Example 1.
  • a 200 dm3 capacity stainless steel vessel equipped with a steam jacket was charged with compounds in the following order: 53.5 kg of the titanium hydroxide gel used in Example 1, the same amount of pure water, 9.5 kg of a silica sol article as shown in Table 1 having a mean particle size of 17 nm (Cataloid S-20L, manufactured by Catalysts & Chemicals Industries Co., Ltd.; SiO2 contents, 20.5% by weight), 2.95 kg of a vanadyl sulfate aqueous solution containing 19.3% by weight of vanadium as V2O5, 0.45 kg of potassium sulfate crystals (purity, 99% by weight), 0.37 kg of ammonium sulfate crystals and 30 kg of a boric acid aqueous solution containing 1.6% by weight of boron as B2O3.
  • Cataloid S-20L manufactured by Catalysts & Chemicals Industries Co., Ltd.
  • SiO2 contents 20.5% by weight
  • the resulting slurry was concentrated to a level of 16% by weight as "TiO2 + SiO2 + V2O5 + K2SO4 + SO3 + B2O3", and the concentrated slurry was subjected to spray drying and drying/calcination steps in the same manner as in Example 1 to obtain catalyst I, with its chemical composition and physical properties shown in Table 2.
  • a tank charged with 53.5 kg of the above titanium hydroxide gel was further charged with 5.6 kg of a silica sol article having a mean particle size of 26 nm (Cataloid SI-50; cf. Table 1 for its properties) which has been passed through a cation exchange resin layer to remove Na, 2.7 kg of a vanadyl sulfate aqueous solution, 1.0 kg of cesium sulfate, 0.35 kg of ammonium sulfate crystals and 30.5 kg of a boric acid aqueous solution (contents as B2O3, 1.6% by weight), and the resulting mixture was treated in the same manner as in Example 1 to obtain catalyst J, with its chemical composition and physical properties shown in Table 2.
  • Cataloid SI-50 cf. Table 1 for its properties
  • Catalyst L was prepared by repeating the process for the production of catalyst A in Example 1 using the same titanium hydroxide gel except that the silica sol article was not used. Chemical composition and physical properties of this catalyst are shown in Table 2.
  • a mixture of 500 kg of a titanyl sulfate aqueous solution containing 5% by weight of titanium as TiO2 with 80.6 kg of an Na-removed silica sol having an SiO2 concentration of 10.3% by weight obtained from a silica gel article (Cataloid SI-550; cf. Table 1) was cooled to 10°C and then neutralized by gradually adding 128 kg of 15% by weight aqueous ammonia spending about 13 minutes with thorough stirring to obtain a coprecipitation gel of titanium hydroxide and silica.
  • the thus obtained gel showed a pH value of 9.1 and a temperature of 22°C.
  • the gel slurry thus obtained was subjected to dehydration and washing using a plate filter. Concentration of solid contents in the thus purified coprecipitation gel was found to be 9.5% by weight.
  • the crystallite diameter of anatase type titanium oxide in the resulting powder was found to be 4.0 nm.
  • pure water was added to 350 kg of the coprecipitation gel to obtain a gel slurry containing 5% by weight of solid contents.
  • the resulting slurry was mixed thoroughly with 120 kg of the aforementioned Na-removed silica sol, 15.0 kg of a vanadyl sulfate aqueous solution, 5.0 kg of a Cs2SO4 aqueous solution, 2.0 kg of ammonium sulfate crystals and 175 kg of a 2.8% by weight boric acid aqueous solution.
  • the thus obtained slurry mixture was heated to evaporate water and concentrate the slurry to a level of 17.8% by weight as "TiO2 + SiO2 + V2O5 + Cs2SO4 + SO3 + B2O3". Thereafter, the concentrated slurry was subjected to spray drying and calcination in the same manner as in Example 1 to obtain a catalyst which was named catalyst M. Chemical composition and physical properties of this catalyst are shown in Table 2.
  • a mixture was prepared from the titanium hydroxide gel, silica sol, vanadyl sulfate aqueous solution, cesium sulfate aqueous solution, ammonium sulfate crystals and boric acid aqueous solution.
  • the mixture was further mixed with a lanthanum nitrate aqueous solution and then subjected to spray drying and calcination to obtain catalyst N, with its chemical composition and physical properties shown in Table 2.
  • Catalysts A to N obtained in Examples 1 to 11 and Comparative Examples 1 to 3 were subjected to a production test of phthalic anhydride from o-xylene by means of a gas phase oxidation using a fluidized bed reactor (made of SUS 304 stainless steel, 83 mm ⁇ x 3400 mmL), with the results shown in Table 3. Unreacted o-xylene and reaction products including phthalic anhydride, phthalides, trialdehydes, maleic anhydride and CO + CO2 were analyzed by gas chromatography.
  • Example 12 A production test of phthalic anhydride from naphthalene by means of a gas phase contact oxidation was carried out using the same fluidized bed reactor used in Example 12, with the results shown in Table 3. Analysis and calculation of the results were carried out in the same manner as in the case of Example 12.
  • catalyst L which does not contain SiO2 in its carrier cannot be used suitably as a fluid catalyst because of its markedly high bulk density.
  • catalyst D which contains no B2O3 in its carrier has extremely large specific surface area and markedly high abrasion rate (low abrasion resistance or weak strength), thus showing considerably low product selectivity. Too much content of B2O3 (catalyst E or Comparative Example 2), however, showed a high bulk density and a low pore volume and resulted in a low product yield.
  • a catalyst which is possessed of not only high activity, high product selectivity and high abrasion resistance (strength) but also suitable bulk density for fluidization, while these excellent properties cannot be found in commonly used catalysts for use in the production of carboxylic anhydrides from hydrocarbons such as o-xylene and naphthalene by means of fluidized bed gas phase oxidation.

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Claims (11)

  1. Catalyseur en lit fluidisé utilisable pour l'oxydation en phase gazeuse d'un hydrocarbure aromatique, essentiellement constitué de 50 à 95 % en poids calculés en TiO₂ + SiO₂ + B₂O₃ du constituant (A) qui comprend du dioxyde de titane, du dioxyde de silicium et de l'oxyde de bore, et
       5 à 50 % en poids calculés en V₂O₅ + M₂O (M représente un métal alcalin) + SO₃ du constituant (B) comprenant de l'oxyde de vanadium, un oxyde de métal alcalin et de l'anhydride sulfurique,
       dans lequel ce V₂O₅ contenu dans le catalyseur est dans l'intervalle compris entre 1 et 30 % en poids, et
       lorsque le constituant (A) est calculé par TiO₂ + SiO₂ + B₂O₃ les rapports pondéraux de B₂O₃ à TiO₂ et de SiO₂ à TiO₂ dans ce constituant (A) sont dans l'intervalle compris entre 0,02 et 0,5 et entre 0,25 et 1,0, respectivement, et
       lorsque le constituant (B) est calculé par V₂O₅ + M₂O + SO₃, les rapports pondéraux de SO₃ à M₂O et de M₂O à V₂O₅ dans ce constituant (B) sont dans l'intervalle compris entre 0,1 et 6,0 et entre 0,1 à 5,0, respectivement.
  2. Catalyseur en lit fluidisé selon la revendication 1, dans lequel cet oxyde de métal alcalin est au moins un oxyde d'un métal alcalin choisi parmi le potassium, le césium et le rubidium.
  3. Catalyseur en lit fluidisé selon la revendication 1, dans lequel ce catalyseur a une masse volumique non tassée de 0,5 à 1,3 g/cm³, une surface spécifique de 5 à 60 m²/g, un volume de pores de 0,1 à 0,6 cm³/g, une usure par frottement ne dépassant pas 5 % en poids pour 15 heures et une taille moyenne en poids des particules de 40 à 150 µm.
  4. Procédé de préparation du catalyseur en lit fluidisé selon la revendication 1, qui comprend les étapes consistant à
    (a) mélanger des composés solubles dans l'eau comme sources respectives de dioxyde de titane, de dioxyde de silicium, d'oxyde de bore, d'oxyde de vanadium, d'oxyde de métal alcalin et d'anhydride sulfurique, simultanément ou dans une combinaison facultative,
    (b) sécher par pulvérisation le mélange de l'étape (a), et
    (c) calciner la poudre séchée par pulvérisation de l'étape (b).
  5. Procédé selon la revendication 4, dans lequel cette source de dioxyde de titane est un hydroxyde de titane qui est capable de former un oxyde de titane ayant un diamètre de cristallite non supérieur à 30 nm lorsqu'il est séché à une température d'environ 300°C.
  6. Procédé selon la revendication 4, dans lequel cette source de dioxyde de silicium est la silice colloïdale.
  7. Procédé selon la revendication 4, dans lequel cette source d'oxyde de vanadium est un composé choisi dans le groupe comprenant le sulfate de vanadyle, le métavanadate d'ammonium et l'oxalate de vanadyle.
  8. Procédé selon la revendication 4, dans lequel cette source d'oxyde de métal alcalin est un composé choisi dans le groupe comprenant les hydroxydes, les sulfates et les carbonates de potassium, césium et rubidium.
  9. Procédé selon la revendication 4, dans lequel cette source d'anhydride sulfurique est l'acide sulfurique ou le sulfate d'ammonium.
  10. Procédé selon la revendication 4, dans lequel cette source d'oxyde de bore est l'acide borique ou le métaborate d'ammonium.
  11. Procédé de préparation d'un anhydride carboxylique qui comprend le fait d'effectuer une oxydation en phase gazeuse d'un hydrocarbure aromatique en présence du catalyseur en lit fluidisé selon la revendication 1.
EP91104826A 1990-03-27 1991-03-26 Catalyseur fluide pour utilisation dans l'oxidation gazeuse d'hydrocarbures aromatiques Expired - Lifetime EP0451614B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
JP77233/90 1990-03-27
JP2077233A JPH0757318B2 (ja) 1990-03-27 1990-03-27 芳香族炭化水素の気相接触酸化用流動触媒およびその製造方法

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EP0451614A1 EP0451614A1 (fr) 1991-10-16
EP0451614B1 true EP0451614B1 (fr) 1994-05-18

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US (1) US5185309A (fr)
EP (1) EP0451614B1 (fr)
JP (1) JPH0757318B2 (fr)
KR (1) KR940000863B1 (fr)
CN (1) CN1029593C (fr)
CA (1) CA2039043C (fr)
DE (1) DE69102007T2 (fr)
NZ (1) NZ237554A (fr)

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6083859A (en) * 1996-06-19 2000-07-04 Degussa-Huls Ag Boron oxide-silicon dioxide mixed oxide
US11289700B2 (en) 2016-06-28 2022-03-29 The Research Foundation For The State University Of New York KVOPO4 cathode for sodium ion batteries
WO2020049462A1 (fr) * 2018-09-05 2020-03-12 Sabic Global Technologies B.V. Catalyseur supporté à l'oxyde de vanadium pour la déshydrogénation d'alcane

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1129475A (en) * 1964-11-10 1968-10-09 Ici Ltd Catalyst
GB1368626A (en) * 1970-08-26 1974-10-02 Rhone Progil Catalyst for the oxidation of ortho-xylene to phthalic anhydride
JPS5210831B1 (fr) * 1971-07-21 1977-03-26
JPS53110986A (en) * 1977-03-09 1978-09-28 Sakai Chem Ind Co Ltd Production of carrier
US4397768A (en) * 1981-02-26 1983-08-09 Oxidaciones Organicas, C.A. "Oxidor" Supported catalyst for the preparation of phthalic anhydride
US4389336A (en) * 1981-09-17 1983-06-21 Koppers Company, Inc. Preparation of naphthalene-oxidation catalyst by impregnation of silica with aqueous solution of VOC2 O4 --K2 SO4 --KHSO4

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CA2039043C (fr) 1995-09-12
JPH0757318B2 (ja) 1995-06-21
DE69102007T2 (de) 1994-09-01
NZ237554A (en) 1992-07-28
EP0451614A1 (fr) 1991-10-16
KR940000863B1 (ko) 1994-02-03
CA2039043A1 (fr) 1991-09-28
CN1056066A (zh) 1991-11-13
KR910016377A (ko) 1991-11-05
US5185309A (en) 1993-02-09
DE69102007D1 (de) 1994-06-23
CN1029593C (zh) 1995-08-30
JPH03278842A (ja) 1991-12-10

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